CN205747681U - The cryogenic separation recovery system of polyolefin row's torch gas - Google Patents
The cryogenic separation recovery system of polyolefin row's torch gas Download PDFInfo
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Abstract
This utility model provides the cryogenic separation recovery system of a kind of polyolefin row's torch gas, it includes being communicated to the exsiccator 110 of plate-fin heat exchanger 120, gas-liquid separator 130, cryopump 140, nitrogen compressor 150 and turbo-expander 160, row's torch gas drying device 110 is delivered to plate-fin heat exchanger 120 after processing and is lowered the temperature, thereafter deliver to gas-liquid separator 130 and carry out gas-liquid separation, gas phase delivers to post-processing unit after plate-fin heat exchanger 120 rewarming, liquid phase after cryopump 140 supercharging through plate-fin heat exchanger 120 rewarming Returning reacting system；Low-pressure nitrogen delivers to plate-fin heat exchanger 120 pre-cooling after nitrogen compressor 150 supercharging, expands through turbo-expander 160, lowers the temperature after it, returns again to plate-fin heat exchanger 120 rewarming to send into nitrogen compressor 150 after room temperature and enters interruption-forming circularly cooling.The hydrocarbons in the row's of recovery torch gas can be maximized, it is simple to downstream utilizes.
Description
Technical field
This utility model relates to the environmental technology field of petroleum chemical industry, particularly relates to the cryogenic separation recovery system of a kind of polyolefin row's torch gas.
Background technology
Polyolefin is the macromolecular compound formed through sudden reaction by many identical or different simple olefins molecules (such as ethylene, propylene, 1-butylene, 1-amylene etc.), wherein mostly important with polyethylene and polypropylene.Due to abundant raw material, cheap, be easily worked molding, high comprehensive performance, polyolefin produce and life every field all have a wide range of applications.Polyolefinic production method has high pressure polymerisation and low-pressure polymerization (including solwution method, slurry method, substance law, vapor phase method).
Polyolefinic production is usually present a common problem, has a large amount of discharge gas to produce the most in process of production, as discharged reaction periodic off-gases in order to control the content of noble gas in polymerization process from reactor.These discharge gas are essentially from devices such as reactor, flash tank, degassing cabins, containing a large amount of unreacted olefinic monomers, comonomer, hydrogen, nitrogen, byproduct of reaction, alkane impurity and induced condensing agent.In order to improve raw material availability, reducing production cost, above-mentioned discharge gas needs to take certain technological means, reclaims active component therein and sends response system back to, and fixed gas is then emitted into torch burning and processes (this portion gas referred to as arranges torch gas).Traditional recovery process typically uses compression condensation method, its flow process condenses high pressure condensation for first low pressure again, i.e. discharge gas first sends into low pressure drainer after low-pressure condenser is cooled to uniform temperature (generally-5 DEG C), uncooled gas is then by compressor boost, high pressure drainer is sent into after high pressure condenser is cooled to uniform temperature (generally-10 DEG C), the high pressure condensed fluid of isolated and low pressure cold lime set send response system back to, and fixed gas is then discharged into torch.
At ambient pressure, the boiling point of ethylene is-103.9 DEG C, and the boiling point of propylene is-47.4 DEG C, and the boiling point of 1-butylene is-6.3 DEG C.Obviously, compression condensation method can realize the preliminary of discharge gas is reclaimed (C4 and above component), and relatively low component such as the ethylene, propylene of boiling point is then only capable of reclaiming a part, and major part is all as arranging torch gas burn processing.Wherein, ethylene/propene is the primary raw material of polyethylene/polypropylene, directly burns unfortunately.Then researcher is had to propose " compression condensation+membrance separation " integrated method to improve the organic efficiency of light hydrocarbon component, as United States Patent (USP) US 5769927 proposes to be used for the method polypropylene effluent gas recovery, but the effect of membrance separation is only concentration, Rich propylene also needs to return compression further, condensation, thus circulating load is more than initial ejection amount, this causes compression and the corresponding equipment investment of condensation phase and energy consumption all to dramatically increase；Chinese patent CN1228366C proposes the method that " compression condensation+vacuum recovery+membrance separation " is integrated, according to patent, also has 10～the propylene of 20%, and processing mode is to send into the burning of flare stack evacuating pipeline in the exit gas that secondary membrane separates.
Understanding from the above mentioned, after compressed condensation and membrance separation two-step pretreatment, row's torch gas still contains the useful constituents such as olefinic monomer, there is the probability continuing recycling.Then researcher (Chinese patent CN1048417C, CN202485331U, CN103520946B) is had to propose to use the method for cryogenic separation to reclaim lighter hydrocarbons further after membrance separation.Wherein, the cryogenic separation part that patent CN202485331U and CN103520946B provide uses turbine expansion technology to obtain cold, its advantage is to take full advantage of the pressure energy of membrance separation tail gas self, need not additionally increase power-equipment, save equipment investment and occupation of land, the most also reclaim part hydrocarbons in membrance separation tail gas.Only from the point of view of membrance separation tail gas recycle, said method is with the obvious advantage, but (i.e. polyolefin effluent gas recovery system is overall) is analyzed in some larger scope, and its limitation is also apparent from.One, the obtainable cold of system is limited to the operating condition of membrance separation tail gas and expands the requirement of outlet tail gas, it is higher that as relatively low in membrance separation tail gas pressure or expansion exports tail gas pressure requirements, there will be the situation that cold is not enough, thus causing the hydrocarbons response rate to decline, the most exercisable space is less；Its two, expand outlet tail gas pressure low, this causes difficulty to reclaiming further, during as used PSA technology to reclaim the hydrogen in tail gas or nitrogen, needs to set up compressor；Its three, reclaim the hydrocarbons pressure that obtains relatively low, such as Returning reacting system, compressor need to be set up when extraction is gas phase, compressor and heat exchanger need to be set up when extraction is gas-liquid two-phase；They are four years old, production technology, product grade adjust and discharge gas source multiformity result in the operating mode frequent fluctuation arranging torch gas, pressure is brought to package unit smooth long term running, this is because turbo-expander rotating speed is up to tens thousand of revs/min, when exhaust flow or pressure oscillation cause rotating speed significantly to change, easily cause the rotor failure of turbo-expander.In sum, tail gas directly arranges torch the most upon inflation, reclaim the hydrocarbons that obtains to use as fuel, simultaneously producer to the requirement of the hydrocarbons response rate the highest in the case of, the method for patent CN202485331U and CN103520946B offer just has advantage；Otherwise, although reclamation film separation tail gas itself need not power-equipment, but may need to increase more power-equipment in downstream, and overall energy consumption of adjusting is the lowest with investment.
Utility model content
In view of this, in order to overcome defect and the problem of prior art, this utility model provides the cryogenic separation recovery system of a kind of polyolefin row's torch gas.
A kind of cryogenic separation recovery system of polyolefin row's torch gas, it exsiccator 110 including being communicated to plate-fin heat exchanger 120, gas-liquid separator 130, cryopump 140, nitrogen compressor 150 and turbo-expander 160, row's torch gas is delivered to described plate-fin heat exchanger 120 after described exsiccator 110 processes and is lowered the temperature, thereafter deliver to described gas-liquid separator 130 and carry out gas-liquid separation, gaseous substance delivers to post-processing unit after described plate-fin heat exchanger 120 rewarming, liquid phase substance is back to response system through described plate-fin heat exchanger 120 rewarming after the supercharging of described cryopump 140 again；Low-pressure nitrogen delivers to the pre-cooling of described plate-fin heat exchanger 120 after the supercharging of described nitrogen compressor 150, expand through described turbo-expander 160, lower the temperature after it, return again to described plate-fin heat exchanger 120 rewarming to send into described nitrogen compressor 150 after room temperature and enter interruption-forming circularly cooling.
In this utility model one better embodiment, row's torch gas temperature range of described plate-fin heat exchanger 120 outlet is-50～-150 DEG C.
In this utility model one better embodiment, the inlet pressure ranges of described cryopump 140 is 2MPa～5MPa.
In this utility model one better embodiment, described cryopump 140 is plunger displacement pump or centrifugal pump.
In this utility model one better embodiment, described exsiccator (110), described gas-liquid separator (130), the fire end of described cryopump (140) and described plate-fin heat exchanger (120) collectively forms the feed side of the cryogenic separation recovery system of described polyolefin row's torch gas, described nitrogen compressor (150), the refrigeration end of described turbo-expander (160) and described plate-fin heat exchanger (120) collectively forms the circularly cooling end of the cryogenic separation recovery system of described polyolefin row's torch gas, described feed side and described circularly cooling end are relatively independent.
The cryogenic separation recovery method of a kind of polyolefin row's torch gas, it comprises the steps:
S101, row's torch gas drying device 110 are delivered to plate-fin heat exchanger 120 after processing and are lowered the temperature；
Row's torch gas after S102, cooling is delivered to gas-liquid separator 130 and is carried out gas-liquid separation, gaseous substance delivers to post-processing unit after described plate-fin heat exchanger 120 rewarming, liquid phase substance again through described plate-fin heat exchanger 120 rewarming, is then return to response system after cryopump 140 supercharging；
S103, low-pressure nitrogen deliver to the pre-cooling of described plate-fin heat exchanger 120 after nitrogen compressor 150 supercharging, low-pressure nitrogen after pre-cooling expands through turbo-expander 160, lowers the temperature, returning again to described plate-fin heat exchanger 120 rewarming to room temperature, that sends into thereafter described nitrogen compressor 150 enters interruption-forming circularly cooling.
Relative to prior art, the cryogenic separation recovery system of polyolefin row's torch gas that this utility model provides uses nitrogen circulation expansion process to replace tail gas expansion process, maximize the hydrocarbons in the row's of recovery torch gas, simultaneously facilitate downstream more easily utilize this hydrocarbons and process tail gas further, thus realize the optimized design of recovery system on the whole.
Accompanying drawing explanation
The composition schematic diagram of the cryogenic separation recovery system of polyolefin row's torch gas that Fig. 1 provides for this utility model first embodiment；
The flow chart of the cryogenic separation recovery method of polyolefin row's torch gas that Fig. 2 provides for this utility model the second embodiment.
Detailed description of the invention
For the ease of understanding this utility model, below with reference to relevant drawings, this utility model is described more fully.Accompanying drawing gives better embodiment of the present utility model.These are only preferred embodiment of the present utility model; not thereby the scope of the claims of the present utility model is limited; every equivalent structure utilizing this utility model description and accompanying drawing content to be made or equivalence flow process conversion; or directly or indirectly it is used in other relevant technical fields, the most in like manner it is included in scope of patent protection of the present utility model.
Unless otherwise defined, all of technology used herein and scientific terminology are identical with belonging to the implication that those skilled in the art of the present utility model are generally understood that.It is intended merely to describe the purpose of specific embodiment at term used in the description of the present utility model herein, it is not intended that in limiting this utility model.Term as used herein " and/or " include the arbitrary and all of combination of one or more relevant Listed Items.
Refer to Fig. 1, this utility model first embodiment provides the cryogenic separation recovery system 100 of a kind of polyolefin row's torch gas, it exsiccator 110 including being communicated to plate-fin heat exchanger 120, gas-liquid separator 130, cryopump 140, nitrogen compressor 150 and turbo-expander 160, row's torch gas is delivered to described plate-fin heat exchanger 120 after described exsiccator 110 processes and is lowered the temperature, thereafter deliver to described gas-liquid separator 130 and carry out gas-liquid separation, gaseous substance delivers to post-processing unit after described plate-fin heat exchanger 120 rewarming, liquid phase substance is back to response system through described plate-fin heat exchanger 120 rewarming after the supercharging of described cryopump 140 again；Low-pressure nitrogen delivers to the pre-cooling of described plate-fin heat exchanger 120 after the supercharging of described nitrogen compressor 150, expand through described turbo-expander 160, lower the temperature after it, return again to described plate-fin heat exchanger 120 rewarming to send into described nitrogen compressor 150 after room temperature and enter interruption-forming circularly cooling.
It is understandable that, the fire end of described exsiccator 110, described gas-liquid separator 130, described cryopump 140 and described plate-fin heat exchanger 120 collectively forms the feed side of the cryogenic separation recovery system 100 of described polyolefin row's torch gas, i.e. row's flare gas recovery end；The refrigeration end of described nitrogen compressor 150, described turbo-expander 160 and described plate-fin heat exchanger 120 then collectively forms the circularly cooling end of the cryogenic separation recovery system 100 of described polyolefin row's torch gas；Preferably, described feed side and described circularly cooling end are relatively independent.
In the present embodiment, the entrance of described exsiccator 110 connects row's torch gas, and outlet is by plate-fin heat exchanger described in pipeline communication 120.Material (i.e. arrange torch gas, flow stock 1) from upstream process processes and after described plate-fin heat exchanger 120 cooling, its dew points at normal pressure delivers to described liquefaction separator 130 after being down to-70 DEG C through described exsiccator 110.Specifically, described exsiccator 110 processes qualified material (stream stock 2) and sends into described plate-fin heat exchanger 120, after being cooled to-50～-150 DEG C (depending on actual temp forms according to material) step by step, send into (stream stock 3) described gas-liquid separator 130.
In the present embodiment, the entrance of described gas-liquid separator 130 is by plate-fin heat exchanger 120 described in pipeline communication, discharge the outlet of gaseous substance by plate-fin heat exchanger described in pipeline communication 120, that discharges liquid phase substance exports the entrance by pipeline communication cryopump 140, and the outlet of described cryopump 140 is by plate-fin heat exchanger described in pipeline communication 120.Material is after the gas-liquid separation of described gas-liquid separator 130, the gaseous substance (stream stock 5) (stream stock 7) after described plate-fin heat exchanger 120 rewarming obtained is delivered to subsequent handling and is recycled further, the liquid phase substance (stream stock 4) obtained is after described cryopump 140 is pressurized to 2～3.5Mpa (depending on concrete pressure is according to the needs of response system), again through described plate-fin heat exchanger 120 rewarming (stream stock 8), it is then return to response system.
In the present embodiment, two outlets of described plate-fin heat exchanger 120, respectively by pipeline communication post-processing unit and response system (not shown), carry gaseous substance and liquid phase substance respectively.
In the present embodiment, described plate-fin heat exchanger 120, described nitrogen compressor 150 and described turbo-expander 160 form the passage of nitrogen circulation swell refrigeration by pipeline communication.Low-pressure nitrogen (stream stock 12) is first through the supercharging of described nitrogen compressor 150, deliver to (stream stock 9) described plate-fin heat exchanger 120 pre-cooling (stream stock 10), reduce pressure through described turbo-expander 160, lower the temperature (stream stock 11), it is then back to described plate-fin heat exchanger 120 rewarming to room temperature (stream stock 12), finally sends into the entrance of described nitrogen compressor 150.Constantly moving in circles through said process, the temperature of the nitrogen after expansion is gradually lowered, thus the cryogenic separation recovery system 100 for whole polyolefin row's torch gas provides cold.
It is understood that depending on the particular make-up that row's torch gas temperature of described plate-fin heat exchanger 120 outlet is according to row's torch gas, it is preferable that row's torch gas temperature range of described plate-fin heat exchanger 120 outlet is-50～-150 DEG C.
In the present embodiment, the gaseous substance (tail gas) of described gas-liquid separator 130 isolated does not throttles, and sends the cryogenic separation recovery system 100 of polyolefin row's torch gas with slightly less than charging (row's torch gas) pressure.
In the present embodiment, the liquid phase substance (i.e. liquefied hydrocarbon material) of described gas-liquid separator 130 isolated utilizes described cryopump 140 to realize supercharging, its outlet pressure adjusts according to the needs of response system, generally in the range from 2MPa～5MPa, the inlet pressure ranges of the most described cryopump 140 is 2MPa～5MPa.Certainly, it is not limited to this, it is possible to it is pressurized to tens more than MPa.Preferably, described cryopump 140 is plunger displacement pump or centrifugal pump.
Referring to Fig. 2, this utility model the second embodiment provides the cryogenic separation recovery method of a kind of polyolefin row's torch gas, and it comprises the steps:
S101, row's torch gas drying device 110 are delivered to plate-fin heat exchanger 120 after processing and are lowered the temperature.
I.e. from the i.e. material (i.e. arranging torch gas) of upstream process after described exsiccator 110 processes, deliver to described plate-fin heat exchanger 120 and be cooled to-50～-150 DEG C step by step, to send into described gas-liquid separator 130.In the present embodiment, the dew points at normal pressure of material delivers to described gas-liquid separator 130 after being down to-70 DEG C.
Row's torch gas after S102, cooling is delivered to gas-liquid separator 130 and is carried out gas-liquid separation, gaseous substance delivers to post-processing unit after described plate-fin heat exchanger 120 rewarming, liquid phase substance again through described plate-fin heat exchanger 120 rewarming, is then return to response system after cryopump 140 supercharging.
I.e. the row's torch gas after cooling is after the gas-liquid separation of described gas-liquid separator 130, the gaseous substance obtained is delivered to subsequent handling (post-processing unit) after described plate-fin heat exchanger 120 rewarming and is recycled further, the liquid phase substance obtained is after described cryopump 140 is pressurized to 2～3.5Mpa, again through described plate-fin heat exchanger 120 rewarming, it is then return to response system.
S103, low-pressure nitrogen deliver to the pre-cooling of described plate-fin heat exchanger 120 after nitrogen compressor 150 supercharging, low-pressure nitrogen after pre-cooling expands through turbo-expander 160, lowers the temperature, returning again to described plate-fin heat exchanger 120 rewarming to room temperature, that sends into thereafter described nitrogen compressor 150 enters interruption-forming circularly cooling.
Thus, constantly moving in circles through said process, the temperature of the nitrogen after expansion is gradually lowered, thus the cryogenic separation recovery system 100 for whole polyolefin row's torch gas provides cold.
Embodiment
The discharge gas of certain petro-chemical corporation's full density polythene process units uses compression condensation method to reclaim, exhaust emissions to torch, and wherein the measured value of row's torch gas duty parameter is as shown in table 1.Its pressure limit is 1.1～1.6 (representative value is 1.3) MPa (G), and temperature range is-15～0 (representative value is-10) DEG C, and flow is 900～1200 (representative value is 1045) Nm3/h.
Table 1 row's torch gas composition measured value (v%)
Row's torch gas (stream stock 1) initially enters exsiccator 110 and processes, treat that dew point reaches about-70 DEG C, deliver to plate-fin heat exchanger 120, temperature drops to-120 DEG C step by step, being then sent to gas-liquid separator 130, the gaseous substance of isolated sends battery limit (BL) (stream stock 7) after plate-fin heat exchanger 120 rewarming；Isolated liquid phase substance, after cryopump is pressurized to 3.2MPa (G), delivers to response system (stream stock 8) after plate-fin heat exchanger rewarming.
Row's torch gas respectively obtains tail gas (i.e. gaseous substance flows stock 7) and hydrocarbons (i.e. liquid phase substance flows stock 8) through cryogenic separation device.Wherein the parameter of stream stock 7 is: pressure 1.28MPa (G), temperature 12 DEG C, flow are 873.6Nm3/h, and its composition is as shown in table 2；The parameter wherein flowing stock 8 is pressure 3.2MPa (G), temperature 12 DEG C, flow are 171.4Nm3/h, and its composition is as shown in table 3.
Table 2 tail gas composition (v%)
Table 3 hydrocarbons composition (v%)
The cryogenic separation recovery system 100 understanding described polyolefin row's torch gas can the hydrocarbons in the row's of recovery torch gas well, it is easy to downstream more easily utilize this hydrocarbons and process tail gas further, thus realizes the optimized design of recovery system on the whole.
The cryogenic separation recovery system 100 of the polyolefin row's torch gas that the utility model proposes has the advantage that one, nitrogen expansion cycle refrigeration system are independent of row's torch gas piece-rate system, by charging operating mode influence of fluctuations less (fluctuation caused because of technique, product grade change or other burst reasons), run the most steady, reduce the risk that turbo-expander 160 damages, there is stronger adaptability and reliability.It is two, independent just because of nitrogen expansion cycle refrigeration system, can first run refrigeration system in start-up, after temperature drops to certain value, the more slowly row's of introducing torch gas, can effectively reduce the waste of hydrocarbons.Three, owing to the pressure of discharge gas is less than response system, no matter could Returning reacting system after using which kind of method to reclaim all necessary supercharging of the hydrocarbons obtained；The utility model proposes and use cryopump 140 to realize supercharging under the conditions of hydrocarbons is in low temperature, liquid, compared with the method that then first reducing pressure by regulating flow rewarming again uses compressor boost, at aspects such as investment, occupation of land, energy consumption, safety, all there is great advantage.Four, the nitrogen content in gaseous substance (tail gas) is higher, simultaneously with higher pressure venting, almost without the pressure loss in addition to overcoming the resistance of ducting, tail gas can be facilitated to reclaim further or utilize, as used as de-storehouse gas (feed bin purge gas).Five, the cryogenic separation recovery system 100 of described polyolefin row torch gas is particularly well-suited to the transformation and upgrade of old factory, newly-increased a set of cryogenic separation device after original device, and original device need not do any change；Row's torch gas after processing compressed condensation method or compression condensation blooming separation integrated approach is the most applicable, only need to be slightly modified on design parameter.
It addition, polyethylene and the tail gas of polypropylene production process composition is similar, identical recovery method can be used completely, only difference on design parameter.Therefore the cryogenic separation recovery system 100 of polyolefin of the present utility model row's torch gas is simultaneously suitable for polyethylene and polypropylene row's torch gas and has the effluent gas recovery being approximated to and utilize.Meanwhile, the step of the cryogenic separation recovery method of described polyolefin row torch gas is simple, it is simple to popularization and application.
Embodiment described above only have expressed several embodiments of the present utility model, and it describes more concrete and detailed, but therefore can not be interpreted as the restriction to this utility model the scope of the claims.It should be pointed out that, for the person of ordinary skill of the art, without departing from the concept of the premise utility, it is also possible to make some deformation and improvement, these broadly fall into protection domain of the present utility model.Therefore, the protection domain of this utility model patent should be as the criterion with claims.
Claims (5)
1. the cryogenic separation recovery system of polyolefin row's torch gas, it is characterized in that, including the exsiccator (110) being communicated to plate-fin heat exchanger (120), gas-liquid separator (130), cryopump (140), nitrogen compressor (150) and turbo-expander (160), row's torch gas delivers to described plate-fin heat exchanger (120) cooling after described exsiccator (110) processes, thereafter deliver to described gas-liquid separator (130) and carry out gas-liquid separation, gaseous substance delivers to post-processing unit after described plate-fin heat exchanger (120) rewarming, liquid phase substance is back to response system through described plate-fin heat exchanger (120) rewarming after described cryopump (140) supercharging again；Low-pressure nitrogen delivers to described plate-fin heat exchanger (120) pre-cooling after described nitrogen compressor (150) supercharging, expand through described turbo-expander (160), lower the temperature after it, return again to described plate-fin heat exchanger (120) rewarming to send into described nitrogen compressor (150) after room temperature and enter interruption-forming circularly cooling.
2. the cryogenic separation recovery system of polyolefin row's torch gas as claimed in claim 1, it is characterised in that row's torch gas temperature range that described plate-fin heat exchanger (120) exports is-50～-150 DEG C.
3. the cryogenic separation recovery system of polyolefin row's torch gas as claimed in claim 1, it is characterised in that the inlet pressure ranges of described cryopump (140) is 2MPa～5MPa.
4. the cryogenic separation recovery system of polyolefin row's torch gas as claimed in claim 1, it is characterised in that described cryopump (140) is plunger displacement pump or centrifugal pump.
5. the cryogenic separation recovery system of polyolefin row's torch gas as claimed in claim 1, it is characterized in that, described exsiccator (110), described gas-liquid separator (130), the fire end of described cryopump (140) and described plate-fin heat exchanger (120) collectively forms the feed side of the cryogenic separation recovery system of described polyolefin row's torch gas, described nitrogen compressor (150), the refrigeration end of described turbo-expander (160) and described plate-fin heat exchanger (120) collectively forms the circularly cooling end of the cryogenic separation recovery system of described polyolefin row's torch gas, described feed side and described circularly cooling end are relatively independent.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105509413A (en) * | 2016-01-19 | 2016-04-20 | 中国科学院理化技术研究所 | Cryogenic separation recycling system and method for exhausted polyolefin flare gas |
| CN107513005A (en) * | 2017-09-27 | 2017-12-26 | 中科瑞奥能源科技股份有限公司 | The technique and system of ethene, iso-butane and nitrogen are reclaimed from polyethylene engineering tail gas |
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2016
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105509413A (en) * | 2016-01-19 | 2016-04-20 | 中国科学院理化技术研究所 | Cryogenic separation recycling system and method for exhausted polyolefin flare gas |
| CN105509413B (en) * | 2016-01-19 | 2018-05-22 | 中国科学院理化技术研究所 | Polyolefin arranges the cryogenic separation recovery system and method for torch gas |
| CN107513005A (en) * | 2017-09-27 | 2017-12-26 | 中科瑞奥能源科技股份有限公司 | The technique and system of ethene, iso-butane and nitrogen are reclaimed from polyethylene engineering tail gas |
| CN107513005B (en) * | 2017-09-27 | 2022-11-15 | 中科瑞奥能源科技股份有限公司 | Process and system for recovering ethylene, isobutane and nitrogen from polyethylene engineering tail gas |
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